CN205368255U - Semicontinuous device of mink cell focus lightization in overcritical solvent environment - Google Patents
Semicontinuous device of mink cell focus lightization in overcritical solvent environment Download PDFInfo
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- CN205368255U CN205368255U CN201521137874.8U CN201521137874U CN205368255U CN 205368255 U CN205368255 U CN 205368255U CN 201521137874 U CN201521137874 U CN 201521137874U CN 205368255 U CN205368255 U CN 205368255U
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Abstract
The utility model provides a semicontinuous device of mink cell focus lightization in overcritical solvent environment, semicontinuous device includes reaction unit, solvent preprocessing device and separator, solvent preprocessing device includes solvent storage tank, high performance liquid pump and pre -heater, the exit end of solvent storage tank passes through the pipeline and links to each other with the entry end of dominant reaction ware behind high performance liquid pump, pre -heater. The utility model discloses semicontinuous device of mink cell focus lightization in overcritical solvent environment, with supercritical fluid continuous conveyor to dominant reaction ware, the reinforcing mass transfer process, continuous conveyor has strengthened supercritical fluid's solvability, and light -end products that the schizolysis produced constantly dissolve and get into in the solvent and carry over out of the dominant reaction ware to adjust the heavy oil reaction and remove to the schizolysis direction, promote cracking, restrain condensation reaction.
Description
Technical field
This utility model relates to heavy oil refining technical field, particularly to a kind of semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment.
Background technology
It is known that oil is occupied an leading position in world's energy resource structure, it it is the basis depended on for existence and development of society.Due to factor impacts such as world politics, crude oil price remains at a higher position.And along with the minimizing of crude oil reserve and exhaustive exploitation, crude quality is in continuous decline, high density, and high-sulphur crude oil with poor quality has accounted for 2/3 (as shown in table 1) of world's crude oil reserve.Currently, the lighting of conventional crude inferior heavy and oil product cleans the exploitation that this prominent energy supply and demand contradiction is just promoting the inferior heavy oil of these high viscositys of residual oil, high temperature coal-tar, Colophonium, oil-sand, high content of heteroatoms.The processing upgrading of heavy crude is that 21 century oil refining process develops the grand strategy problem faced, and is also the effective way evading petroleum resources risk.
Table 1. world crude quality is high-sulfurized, heaviness tends to
Traditional mink cell focus processing technique can be divided into two kinds of techniques of decarburization and hydrogenation.Wherein decarbonization process includes the process such as thermal cracking, catalytic cracking.Hydrogenation technique includes the hydrogenation process such as cracking, hydrofinishing.Thermal cracking of heavy oil needs higher temperature, the highest more than 1273K, and along with strong condensation, coking rate may be up to 80%.Compared with thermal cracking, catalytic cracking and hydrogenation process reaction temperature are lower, and selectivity is also better, and lighter products productivity is high, but the catalysqt deactivation caused due to carbon distribution and metal deposit can cause the instability of catalytic cracking and hydrogenation cracking.Additionally, catalytic cracking process, raw oil having higher requirement, heavy crude viscosity is big, and sulfur content is high, it is difficult to meet the catalytic cracking high request to raw material.Temperature, pressure, safety are all required by hydrogenation process, and hydrogen manufacturing workshop section is one of production unit that refinery's cost is the highest so that hydrogenation technique production cost is too high.In addition, some fraction section in heavy oil is only processed by conventional crude oil processing technique, and its heavier component is under-utilized, can cause the waste of the energy.Therefore, the mink cell focus processing technique developing new high-efficiency environment friendly is extremely urgent.
Supercritical fluid (water, methanol, carbon dioxide etc.) has the physicochemical characteristic of liquids and gases concurrently, particularly its solvent power and reactive, diffusion close with liquid and mass transfer characteristics are close to gas, and its surface tension is close to zero, it means that supercritical fluid is a kind of new and effective separating medium and reaction medium.It addition, supercritical fluid technology is in application process, it is easy to reclaiming also can be recycled, does not result in dissolvent residual or serious three-protection design problem, there is the characteristic and advantage of green chemical industry.Prepare at derived energy chemical, micro Nano material, environmental conservation and food safety, field of biological pharmacy have successfully application and wide prospect.
Supercritical water (SupercriticalWater is abbreviated as SCW) has cheap, nontoxic, pollution-free and product and the feature such as is easily isolated.In recent years, SCW technology obtains the extensive attention of researcher, it has proved that have the advantage of uniqueness in extracting coal, oil shale and mink cell focus and producing oil product and type waste plastic oiling etc..Heavy oil reacts in supercritical water and has the advantage that
1) expensive hydrogen and organic solvent is not used just heavy fossil fuel can be carried out lighting, it is expected to reduce cost.Owing to not using hydrogen and organic solvent, not only can reduce green coke but also add safety.
2) condensation reaction is inhibited to make the by-products such as coke reduce.
3) conversion process does not use the organic solvent being likely to cause environmental pollution, and water itself is again cleaning, and reaction is again in completely airtight system, is of value to environmental protection.
4) it is contemplated that there are the heteroatomic probabilities such as elimination sulfur, the fuel that production environment is friendly is conducive to.But, the working condition of SCW upgrading reaction is comparatively harsh: temperature more than 374 DEG C, pressure is more than 22.4MPa；It addition, SCW has stronger corrosivity, it means that the designing requirement for consersion unit is higher, processing cost is also higher；And in process it is possible that inorganic salt precipitation blockage problem be restriction SCW Technique Popularizing major obstacle.Additionally, be all based on Batch reaction processes, the shortcoming research to tandem reaction sequence about the research of SCW lighting reaction both at home and abroad at present, and the latter is for industrialization, more has realistic meaning.
Research finds, under supercritical cases, the hydroxyl of alcohols can cut off ether bridged bond and make some polymer depolymerization, is widely used to the preparation of oils and fats, PET, the recovery of polyurethane and biodiesel.Therefore this project intends the medium that employing supercritical methanol reacts as lighting.Methanol critical temperature 239 DEG C, pressure 8.1MPa, compared to SCW, critical condition is comparatively gentle；In addition supercritical methanol is without obvious corrosivity, to equipment, pipeline without requirement for anticorrosion, less costly；Equally at supercritical conditions, the dissolubility of larger molecular organics is better than water by methanol, and the hydrogen supply capacity of methanol is worked as with aqueous phase simultaneously.This means: under the premise ensureing identical lighting efficiency, use supercritical methanol will significantly reduce equipment cost and improve process safety, in addition, hydroxyl radical free radical in methanol has extremely strong response characteristic, as the startup free radical in heavy oil thermal cracking process, reaction can be made to carry out at a lower temperature.But the reaction that heavy oil is in supercritical fluid is still thermal cracking processes, and coking is difficult to avoid that.
Utility model content
Technical problem to be solved in the utility model is the drawbacks described above for prior art, a kind of semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment is provided, to strengthen the solvability of supercritical fluid, the light-end products that cracking produces are made constantly to dissolve in entrance solvent and be carried over reactor, move thus regulating heavy oil reaction to cracking direction, promote cracking reaction, it is suppressed that condensation reaction.
To achieve these goals, this utility model provides a kind of semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment, including:
One solvent pre-treatment device, including a solvent tank, efficient liquid phase pump and preheater,
Described efficient liquid phase delivery side of pump end, arrival end are connected with described preheater, described solvent tank respectively, and the port of export of described preheater is connected with the arrival end of described efficient liquid phase pump；
One reaction unit, outlet with described solvent pre-treatment device is connected, described reaction unit farther includes a main reactor and a product surge tank, the port of export of described main reactor is connected with the arrival end of described product surge tank, and the arrival end of described main reactor is connected with the port of export of described preheater；
One segregation apparatus, outlet with described reaction unit is connected, described segregation apparatus farther includes: a water scrubber, a rectifying column and a product storage tank, the arrival end of described water scrubber is connected with the port of export of described product surge tank, the port of export of described water scrubber is connected with the arrival end of the arrival end of described rectifying column, described product storage tank respectively, the gas outlet, top of described rectifying column is connected with described preheater, and the bottom row mouth of a river of described rectifying column is connected with the tower top charging aperture of described water scrubber；
One monitoring device, is connected with described main reactor, described preheater connection.
The described semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment, the outside of described main reactor is provided with dismountable electric heating chuck.
The described semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment, described monitoring device includes a temperature measuring equipment, a pressure tester, a controller, described temperature measuring equipment, described pressure tester are connected with the arrival end of described main reactor, the port of export respectively, and described temperature measuring equipment, described pressure tester are all electrical connected with described controller.
The described semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment, the port of export of described preheater includes first port of export, second port of export, described first port of export is connected with the arrival end of described main reactor, described second port of export respectively with the arrival end of described efficient liquid phase pump, described temperature measuring equipment connects, described pressure tester connects, the arrival end of described preheater includes the first arrival end, second arrival end, described first arrival end is connected with described efficient liquid phase delivery side of pump end, described second arrival end is connected with the gas outlet, top of described rectifying column.
The described semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment, described temperature measuring equipment is internal with described main reactor to be connected.
The described semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment, the port of export of described water scrubber includes the 3rd port of export, the 4th port of export, described 3rd port of export is connected with the arrival end of described rectifying column, and described 4th port of export is connected with the arrival end of described product storage tank.
The described semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment, described product storage tank is arranged on weighing balance
The described semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment, the upper cover of described main reactor, under cover and be equipped with sintered plate.
The described semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment, the upper cover of described main reactor, under cover and be equipped with sintered plate.
The described semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment, the weldering of described sintered plate is arranged at the inner side of described upper cover, lower cover.
The described semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment, described sintered plate is sintered by the glass plate being coated with adsorbent and glass dust and forms.
The described semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment, the pipe range 1～1.2m of described preheater, diameter is 0.5～0.8mm.
Beneficial functional of the present utility model is in that:
The semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment of this utility model design, supercritical fluid is obtained by heater heating, and supercritical fluid is delivered to continuously main reactor, mass transfer enhancement process, conveying enhances the solvability of supercritical fluid continuously；Supercritical fluid time of staying in reactor is shorter, it is dissolved in light-end products therein to be difficult to after polymerization reaction, and the light-end products cracking generation constantly dissolve in entrance solvent and are carried over main reactor, move thus regulating heavy oil reaction to cracking direction, promote cracking reaction, it is suppressed that condensation reaction.
Below in conjunction with the drawings and specific embodiments, this utility model is described in detail, but not as to restriction of the present utility model.
Accompanying drawing explanation
Fig. 1 is the semi-continuous apparatus structural representation of this utility model one embodiment；
Fig. 2 A is the structural representation of the main reactor upper cover of this utility model one embodiment；
Fig. 2 B is the right view of the main reactor upper cover of this utility model one embodiment；
Fig. 3 A is the structural representation of the main reactor of this utility model one embodiment；
Fig. 3 B is the left view of the main reactor of this utility model one embodiment.
Wherein, accompanying drawing labelling
Solvent tank 1
Efficient liquid phase pump 2
Preheater 3
First port of export 31
Second port of export 32
First arrival end 33
Second arrival end 34
Main reactor 4
Sintered plate 41
The arrival end 42 of main reactor
The port of export 43 of main reactor
Upper cover 44
Lower cover 45
Product surge tank 5
Water scrubber 6
3rd port of export 61
4th port of export 62
Rectifying column 7
Product storage tank 8
Temperature measuring equipment 9
Pressure tester 10
Controller 11
Weighing balance 12
Detailed description of the invention
Referring to Fig. 1, Fig. 1 is the structural representation of this utility model one embodiment, the semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment of the present utility model, for light materialization of heavy oil, its structure includes reaction unit, solvent pre-treatment device, segregation apparatus and monitoring device, the gateway of reaction unit is connected with segregation apparatus, solvent pre-treatment device respectively, and monitoring device is connected with reaction unit, solvent pre-treatment device respectively.
One reaction unit includes main reactor 4 and product surge tank 5, the port of export 43 of main reactor is connected with the arrival end of product surge tank 5 by pipeline, the upper cover 44 of main reactor 4, lower cover 45 are equipped with sintered plate, main reactor reaction under environment under high pressure can be met, upper cover 44 ensures passing through of solvent, lower cover 45 ensures that the supercritical fluid dissolving light-end products can pass through, and reaction dissolvent enters main reactor 4 by the sintered plate of inlet duct.Constantly the supercritical methanol of flowing is carried dissolving light components therein secretly and is entered product surge tank through the sintered plate being welded on lower cover 45 by the outlet conduit of main reactor 4, sintered plate weldering is arranged at the inner side of upper cover 44, lower cover 45, and sintered plate is sintered by the glass plate being coated with adsorbent and glass dust and forms.
One solvent pre-treatment device includes solvent tank 1, efficient liquid phase pump 2 and preheater 3, the discharging opening of solvent tank 1 passes through pipeline through efficient liquid phase pump 2, after preheater 3, the arrival end 42 with main reactor is connected, preheater 3 is provided with first port of export 31, second port of export 32, first port of export 31 arrival end 42 by pipeline with main reactor, monitoring device connects, second port of export 32 is connected with the arrival end of efficient liquid phase pump 2 by pipeline, or the second outlet 32 ends are connected by the pipeline between pipeline with efficient liquid phase pump 2 and solvent tank 1, preheater 3 is also provided with the first arrival end 33, second arrival end 34, first arrival end 33 is connected with the port of export of efficient liquid phase pump 2 by pipeline, second arrival end 34 is connected with segregation apparatus by pipeline.Pipe range 1～the 1.2m of the preheater 3 that this utility model adopts, diameter is 0.5～0.8mm.
One segregation apparatus includes water scrubber 6, rectifying column 7 and product storage tank 8, the arrival end of water scrubber 6 is connected with the port of export of product surge tank 5 by pipeline, water scrubber 6 is provided with the 3rd port of export the 61, the 4th port of export 62,3rd port of export 61 is connected with the arrival end of rectifying column 7 by pipeline, 3rd port of export 61 is positioned at the bottom of rectifying column 7,4th port of export 62 is connected with product storage tank 8 by pipeline, and the 4th port of export 62 is positioned at the middle and lower part of rectifying column 7.The gas outlet, top of rectifying column 7 is connected with the second arrival end 34 of preheater 3 by pipeline, and the bottom row mouth of a river of rectifying column 7 is connected with the tower top charging aperture of water scrubber 6 by pipeline, and wherein product storage tank 8 is arranged at weighing balance.
One monitoring device includes temperature measuring equipment 9, pressure tester 10, controller 11, temperature measuring equipment 9, pressure tester 10 are connected with first port of export 31 of the gateway end of main reactor 4, preheater 3 respectively, and temperature measuring equipment 9, pressure tester 10 are all electrical connected with controller 11.The temperature probe of temperature measuring equipment 9 is respectively arranged at first port of export 31 of the gateway end of main reactor 4, main reactor 4 inside and preheater 3, the pressure transducer of pressure tester 10 is also respectively arranged at first port of export 31 of the gateway end of main reactor 4, preheater 3, temperature probe, pressure sensor monitoring temperature, pressure data, temperature measuring equipment 9, pressure tester 10 send temperature, pressure data to controller 11 (such as computer), in order to monitor the temperature of whole course of reaction.
When reaction starts, the mixture of methanol Yu heavy oil is placed in main reactor 4, makes main reactor 4 be warming up to 350 DEG C by the electric heating chuck outside main reactor 4 and react.Methanol is squeezed into preheater 3 by efficient liquid phase pump 2 in solvent tank 1, the temperature arranging preheater 3 is 300 DEG C, and after temperature reaches 300 DEG C, methanol reaches supercriticality, open flow control valve, enable supercritical methanol to pass the heavy oil in main reactor 4.In main reactor 4, the medium that supercritical methanol reacts as lighting, it is delivered to continuously in main reactor 4.Methanol cracks the OH of generation at supercritical conditions and has extremely strong reactivity, can as the cracking process starting free radical activation heavy oil product, and conveying enhances the solvability of supercritical methanol continuously, the light-end products that cracking produces constantly dissolve in entrance solvent and are carried over main reactor 4, it is dissolved in light-end products therein to be difficult to after polymerization reaction, moving to cracking direction thus regulating heavy oil reaction, promoting cracking reaction, it is suppressed that condensation reaction.
In main reactor 4 after reaction, the methanol dissolving light-end products enters water scrubber 6 through product surge tank 5, and in water scrubber 6, methanol is dissolved in the water and separates with oil product, and the oil product after removing methanol is collected in product storage tank 8 and is processed further.In water scrubber 6, the aqueous solution of methanol enters rectifying column 7, is separated by rectification at rectifying column 7, and methanol follows swap-in from tower top discharge as circulating solvent and enters preheater 3, again participates in reaction after the heating of preheated device 3, and the water return water scrubber 6 at the bottom of rectifying column 7 tower does washing and uses.When the product weight in product storage tank 8 is not further added by, stopped reaction, change raw material.
Claims (11)
1. the semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment, it is characterised in that including:
One solvent pre-treatment device, including a solvent tank, efficient liquid phase pump and preheater,
Described efficient liquid phase delivery side of pump end and arrival end are connected with described preheater, described solvent tank respectively, and the port of export of described preheater is connected with the arrival end of described efficient liquid phase pump；
One reaction unit, outlet with described solvent pre-treatment device is connected, described reaction unit farther includes a main reactor and a product surge tank, the port of export of described main reactor is connected with the arrival end of described product surge tank, and the arrival end of described main reactor is connected with the port of export of described preheater；
One segregation apparatus, outlet with described reaction unit is connected, described segregation apparatus farther includes: a water scrubber, a rectifying column and a product storage tank, the arrival end of described water scrubber is connected with the port of export of described product surge tank, the port of export of described water scrubber is connected with the arrival end of the arrival end of described rectifying column, described product storage tank respectively, the gas outlet, top of described rectifying column is connected with described preheater, and the bottom row mouth of a river of described rectifying column is connected with the tower top charging aperture of described water scrubber；
One monitoring device, is connected with described main reactor, described preheater connection.
2. the semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment as claimed in claim 1, it is characterised in that the outside of described main reactor is provided with dismountable electric heating chuck.
3. the semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment as claimed in claim 1, it is characterized in that, described monitoring device includes a temperature measuring equipment, a pressure tester, a controller, described temperature measuring equipment, described pressure tester are connected with the arrival end of described main reactor, the port of export respectively, and described temperature measuring equipment, described pressure tester are all electrical connected with described controller.
4. the semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment as claimed in claim 3, it is characterised in that described temperature measuring equipment is internal with described main reactor to be connected.
5. the semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment as claimed in claim 3, it is characterized in that, the port of export of described preheater includes first port of export, second port of export, described first port of export is connected with the arrival end of described main reactor, described second port of export respectively with the arrival end of described efficient liquid phase pump, described temperature measuring equipment connects, described pressure tester connects, the arrival end of described preheater includes the first arrival end, second arrival end, described first arrival end is connected with described efficient liquid phase delivery side of pump end, described second arrival end is connected with the gas outlet, top of described rectifying column.
6. the semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment as claimed in claim 1, it is characterized in that, the port of export of described water scrubber includes the 3rd port of export, the 4th port of export, described 3rd port of export is connected with the arrival end of described rectifying column, and described 4th port of export is connected with the arrival end of described product storage tank.
7. the semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment as claimed in claim 1, it is characterised in that described product storage tank is arranged on weighing balance.
8. the semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment as claimed in claim 1, it is characterised in that the upper cover of described main reactor, under cover and be equipped with sintered plate.
9. the semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment as claimed in claim 8, it is characterised in that the weldering of described sintered plate is arranged at the inner side of described upper cover, lower cover.
10. the semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment as claimed in claim 9, it is characterised in that described sintered plate is sintered by the glass plate being coated with adsorbent and glass dust and forms.
11. the semi-continuous apparatus of light materialization of heavy oil in supercritical solvent environment as claimed in claim 1, it is characterised in that the pipe range 1～1.2m of described preheater, diameter is 0.5～0.8mm.
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| CN201521137874.8U CN205368255U (en) | 2015-12-31 | 2015-12-31 | Semicontinuous device of mink cell focus lightization in overcritical solvent environment |
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| CN201521137874.8U CN205368255U (en) | 2015-12-31 | 2015-12-31 | Semicontinuous device of mink cell focus lightization in overcritical solvent environment |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107841333A (en) * | 2017-11-30 | 2018-03-27 | 华东理工大学 | Method and corresponding crude oil for pour point depression of crude oil |
| CN109211721A (en) * | 2017-07-06 | 2019-01-15 | 中国石油天然气股份有限公司 | A kind of experimental provision |
| CN109609183A (en) * | 2018-12-11 | 2019-04-12 | 西安交通大学 | Coal tar Method for treatment of oil based on supercritical methanol |
| CN111690429A (en) * | 2019-03-15 | 2020-09-22 | 中国石油天然气股份有限公司 | Supercritical hydrothermal viscosity reduction method for oil sand asphalt |
| US11255832B2 (en) | 2017-07-06 | 2022-02-22 | Petrochina Company Limited | Device and method for determining solubility of elemental sulfur in sulfur-containing gas |
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2015
- 2015-12-31 CN CN201521137874.8U patent/CN205368255U/en active Active
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109211721A (en) * | 2017-07-06 | 2019-01-15 | 中国石油天然气股份有限公司 | A kind of experimental provision |
| US11255832B2 (en) | 2017-07-06 | 2022-02-22 | Petrochina Company Limited | Device and method for determining solubility of elemental sulfur in sulfur-containing gas |
| CN107841333A (en) * | 2017-11-30 | 2018-03-27 | 华东理工大学 | Method and corresponding crude oil for pour point depression of crude oil |
| CN107841333B (en) * | 2017-11-30 | 2019-06-14 | 华东理工大学 | Method and corresponding crude oil for pour point depression of crude oil |
| CN109609183A (en) * | 2018-12-11 | 2019-04-12 | 西安交通大学 | Coal tar Method for treatment of oil based on supercritical methanol |
| CN111690429A (en) * | 2019-03-15 | 2020-09-22 | 中国石油天然气股份有限公司 | Supercritical hydrothermal viscosity reduction method for oil sand asphalt |
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